Heat exchanger of gas-liquid contacting plate type

Abstract: A heat exchanger (2) of gas-liquid contacting plate type includes: a plurality of heat transfer plates (4), disposed vertically at certain intervals, defining air flow passages therebetween which allow air to rise, and each of the plates (4) has a heat medium flowing passage thereinside for allowing a heat medium (C) to flow therethrough while the side surfaces of each of the heat transfer plates (4), which define the air flow passages, are adhered with nets (30) for allowing a liquid to flow downward along the nets and plates.

Description: The present invention relates to a heat exchanger of plate type, and more detailedly to a heat exchanger of plate type which is able to effectively bring a gas into contact with a liquid on the plate surfaces while performing heat exchange. In typical chemical plants, it is often needed to efficiently bring a gas into contact with a liquid in a short period of time. This situation is represented by, for example, the case where CO 2 (carbon dioxide) gas in a combustion exhaust gas is recollected by an absorbent solution such as amine aqueous solution. In order to fulfill such demands, the applicant of the present invention previously proposed a gas-liquid contacting apparatus which is filled up with a large number of tubular structure fillers, each having a horizontal cross-section of an arbitrary shape and wherein inside walls of the tubular structure is vertically arranged forming gas-liquid contact surfaces so that the gas-liquid contact surfaces may be disposed in parallel with the flow of the gas and wherein the liquid supplied from a site above the fillers is made to flow downward along the gas-liquid contact surfaces while the gas is supplied from a site under the fillers so as to contact the gas with the liquid by feeding the gas from a site under the fillers, the apparatus being characterized in that the gas-liquid contact surface is made up of a plate-like member with net-like members adhered onto the surfaces thereof. In the gas-liquid contacting apparatus of the above proposal, in the case where the gas is of the combustion exhaust gas and the liquid is of the amine aqueous solution as stated above, the absorbent liquid is increased in temperature by the heat of reaction as the liquid absorbs CO 2 gas, resulting in a decreased reaction rate of absorption. To deal with this, a separately provided heat exchanger (a cooler) was provided for the apparatus to properly adjust the supplied absorbent liquid in temperature. Nevertheless, as flowing downward in the gas-liquid contacting apparatus, the reacting liquid increases in temperature, so that the equilibrium constant for the absorption reaction tends to lower, though the velocity of reaction increases. As a result, only the adjustment in temperature of the absorbent liquid supplied was not effective enough to afford appropriate measure for adjusting the reaction rate. As seen in this example, since, in chemical plants, the gas-liquid contact process typically involves exothermic and/or endothermic reaction, each step requires separate cooler, heater, heat exchanger etc., for the liquid and/or gas used. Further, in view of heat exchange efficiency, alternatively, in consideration of increase in cost for building the plant due to the complication of the plant structure as well as due to the augment of the required space, the improvement of the gas-liquid contacting apparatus has been earnestly desired. Under consideration of what is discussed above, the present inventors hereof have energetically made studies on the apparatus which is able to perform heat exchange and which is advantageous in view of the heat exchange efficiency and space saving, and consequently found heat exchanger having a certain structure as being extremely effective, to thereby complete the present invention. In the present invention as claimed, a heat exchanger of gas-liquid contacting plate type is provided which can perform both the gas-liquid contact process and the heat exchange process simultaneously, and is advantageous in view of heat exchange efficiency and space factor of the apparatus. A feature of the present invention resides in that a heat exchanger of gas-liquid contacting plate type comprises: a plurality of heat transfer plates, disposed vertically at certain intervals, defining air flow passages therebetween which allow air to rise, and is constructed such that each of the plates has a heat medium flowing passage thereinside for allowing a heat medium to flow therethrough and the side surfaces of each of the heat transfer plates, which define the air flow passages, are adhered with nets for allowing a liquid to flow downward along the nets and plates. In accordance with this aspect of the present invention, a liquid to be subjected to the gas-liquid contact flows downward along the nets adhered to the side faces of the heat transfer plates. In this while, the liquid flowing downward flows down at slow speeds since many micro regions existing in acute forms between the meshes of the nets and the heat transfer plate make the liquid stay temporarily and since the existence of meshes of the nets causes the liquid flowing downward along the heat transfer plates to spread horizontally, not allowing the liquid to collecting on particular spots. In addition, as a result of the nets being adhered to the heat transfer plates, the surface of the liquid staying at meshes is successively renewed or replaced by the liquid flowing downward, so that the liquid is highly efficiently brought into contact with a gas rising from a site below through passages between the heat transfer plates. In addition, the exothermic or endothermic heat usually accompanied by the gas-liquid contact process can be taken off directly at positions where it is generated by the heat medium inside the heat transfer plates, achieving highly efficient heat exchange. In consequence, it is possible to provide a gas-liquid contacting heat exchanger which presents markedly excellent performances by virtue of both the high gas-liquid contact efficiency and the high heat exchange efficiency. Further scope of applicability of the present invention will become apparent from the detailed description given hereinafter. However, it should be understood that the detailed description and specific examples, while indicating preferred embodiments of the invention, are give by way of illustration only, since various changes and modifications within the spirit and scope of the invention will become apparent to those skilled in the art from this detailed description. BRIEF DESCRIPTION OF THE DRAWINGS The present invention will become more fully understood from the detailed description given hereinbelow and the accompanying drawings which are given by way of illustration only, and thus are not limitative of the present invention and wherein: Fig. 1 is a schematic perspective view showing a heat exchanger of gas-liquid contacting plate type in accordance with the present invention; Fig. 2 is a schematic side section of the heat exchanger of Fig. 4; Fig. 3 is a schematic diagram showing an example of applying a heat exchanger of gas-liquid contacting plate type of the present invention to a CO 2 regeneration tower; Fig. 4 is a sectional view showing an example of a heat exchanger utilizing conventional heat pipes; and Fig. 5 is a perspective view showing a heat exchanger utilizing conventional heat pipes. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Referring to Figs. 1 to 3, a configuration in accordance with an embodiment of the present invention will be described. Initially, Figs. 1 and 2 are to be referred. Figs. 2 and 2 are perspective and side views schematically illustrating a principle of a heat exchanger of gas-liquid contacting plate type. A heat exchanger 2 of gas-liquid contacting plate type in accordance with the present invention is composed of, as shown in figures, a large number of heat transfer plates 4 placed vertically in parallel with one another, passages 10 formed inside the heat transfer plates 4 for introducing a heat medium C, gas passages 20 formed between the heat transfer plates 4, and nets 30 provided on the outside surfaces of the heat transfer plates 4 or on the side surfaces facing the gas passages. The heat transfer plate 4 is made up of a metal having a good thermal conductivity and has hollow inside forming the passage 10 for the heat medium to be described below. Figs.1 and 2 show only three heat transfer plates 4 for simplifying the illustrations, but in practice, a larger number of heat transfer plates 4 are disposed at certain intervals and supported by means of rigidity of pipes 6 or with the help of unillustrated spacers, as required. The insides of these heat transfer plates 4 communicate with each other through the pipes 6, and the heat medium C flows in directions shown by arrows in Fig.2. In the example illustrated, the pipes 6 are connected so that the heat medium C flows in the same direction (downward) through the inside of all the heat transfer plates 4, but it is possible to provide the pipes 6 so as to alternate the directions of flow of the heat medium C inside the plates 4. The heat medium C is unlikely to leak if joints between the heat transfer plates 4 and the pipes 6 are welded, though welding makes it difficult to disassemble the heat exchanger for maintenance. In general, the heat transfer plates 4 and pipes 6 are jointed by fitting gaskets therebetween and fixing with screws etc., in order to make easy the maintenance and repairs of the apparatus. The net 30 adhered to the heat transfer plate 4 is preferably made of a material that will not be eroded by the gas and liquid to be subjected to the gas-liquid contact. For example, the net may be formed by a wire mesh, a plastic net etc. The weaving manner of the net 30 illustrated is plain weave, but this weave is not limited and any other various weaves inclusive of twill weave can be used. No particular restriction is put on a technique for adhering the net 30 onto the heat transfer plate 4. The net 30 may be disposed so that the wires of the net 30 may be placed at a different angle to the ground. The size of the mesh of the net to be selected is preferably 3 mesh or more, more preferably 8 mesh or more. Next, the operation of the thus constructed heat exchanger of gas-liquid contacting plate type will be briefed. In Fig.2, a gas G to be subjected for the gas-liquid contact rises upward through the air passages 20 formed between heat transfer plates 4 while a liquid L for the gas liquid contact is made to flow down cascade-wise from the upper site of the heat transfer plates 4. Since nets 30 are adhered onto the side faces of heat transfer plates 4, the liquid L, as flowing downward along the side faces of heat transfer plates 4, mainly tends to stay in micro regions defined in acute forms between horizontally extending portions of the net 30 and the side surface of the heat transfer plate. Further, as the liquid flows down over the net 30, the surface part of the staying liquid is successively renewed by newly coming liquid. Thus, since the liquid L spreads horizontally and stays and since the surface part of the liquid is successively renewed, the liquid L is exposed on the surfaces of heat transfer plates 4 and may come into contact at a high-efficiency with the gas G rising. On the other hand, the predetermined heat medium C flows inside heat transfer plates 4 so as to directly heat or cool the liquid L flowing downward along the heat transfer plates 4. In the case where only a gas containing a condensible substance is made to pass and be cooled while no liquid L is made to flow down from above the heat transfer plates 4, the condensible component in the gas, e.g., water in a combustion exhaust gas is condensed by taking off the condensing latent heat of the condensible component in the gas by way of the heat medium C inside the heat transfer plates 4. The condensed component then adheres to nets 30 as well as onto the side faces of heat transfer plates 4. As increasing in quantity, the condensed water adhered gradually flows downward. The condensed component spreads laterally over vertical faces formed of the nets 30 and heat transfer plates 4, so as to be brought into contact with the high temperature combustion exhaust gas fed from the lower site of the apparatus. In this way, the combustion exhaust gas may be cooled efficiently. The condensed water component in this case finally drains off downward from the heat exchanger of gas-liquid contacting plate type. Heat transfer caused in the gas-liquid contact process involves, in addition to the condensing latent heat, the heat of reaction arising in the gas-liquid contact. The cases where the reaction is exothermic are represented by the aforementioned case in which CO 2 component in the combustion exhaust gas is absorbed by the amine solution. In such a case, the generated heat is directly taken off by way of the heat medium C flowing inside the heat transfer plates 4, thereby preventing rise in temperature of the contacting gas and liquid so as to avoid lowering of the equilibrium constant. In this way, a highly efficient gas-liquid contacting process can be achieved. In the case of absorbing reaction, the situation becomes opposite, so heat inside the heat transfer plates 4 is transferred to the gas-liquid contact side. Next, referring to Fig.3, description will be made on an example in which the heat exchanger of gas-liquid contacting plate type of the present invention is applied to a regeneration tower for regenerating amine absorbent solution by recollecting CO 2 from the amine absorbent solution which has absorbed CO 2 (to be referred to as CO 2 -rich amine absorbent solution hereinbelow). In this example, the same components with those shown in Figs. 1 and 2 are assigned with the same reference numerals and the nets 30 shown are simplified in the figure. In Fig.3, two heat exchangers of gas-liquid contacting plate type of the present invention are mounted in upper and lower sites inside a regeneration tower 50. In the upper heat exchanger 2a, low-temperature cooling water is introduced as a heat medium in heat transfer plates 4a which constitute the upper heat exchanger 2a, in order that amine contained in a slight amount in the CO 2 gas rising through air passages 20a may be prevented from discharging outside the tower. On the other hand, high-temperature steam is introduced as a heat medium in the heat transfer plates 4b constituting the lower heat exchanger 2b, in order to regenerate the absorbent solution by separating CO 2 from the CO 2 -rich amine absorbent solution. Provided between both the heat exchangers 2a and 2b is a nozzle 52 which sprays over the lower heat exchanger 2b the CO 2 -rich amine absorbent solution delivered from an unillustrated CO 2 absorption tower. An absorbent solution reservoir 54 for receiving regenerated amine absorbent solution having a low concentration of CO 2 is provided at the bottom of the regeneration tower 50. The CO 2 -rich amine absorbent solution sprayed from the nozzle 52, together with condensed water (to be described later) which comes down from the upper heat exchanger 2a, gradually flows downward along heat transfer plates 4b having nets 20 adhered thereto in the lower heat exchanger 2b. In this situation, high-temperature steam circulates inside the heat transfer plates 4b, so that the CO 2 -rich amine absorbent solution is heated efficiently. Therefore, as steam is generated from the amine absorbent solution, gaseous CO 2 is released together with the steam. The gaseous substances, rising through the air passages 20b, are brought into contact with the CO 2 -rich amine absorbent solution since the solution is made to flow down continuously from the upper site. As a result, the steam generated and the CO 2 -rich amine absorbent solution come into contact with one another on heat transfer plates 4b with nets 30 adhered thereto, whereby the CO 2 component is further promoted to separate from the steam, both released from the CO 2 -rich amine absorbent solution. The heat energy required for this process is supplied continuously from the flowing steam inside the heat transfer plates 4b as described above. In consequence, both the gas-liquid contact process and the heat exchange process are simultaneously carried out highly efficiently. The thus regenerated amine aqueous solution with CO 2 component removed therefrom is then temporarily reserved in the recollected solution reservoir 54 disposed in the lower portion. Thereafter, the reserved solution is discharged, as required, by a pump 56 into the absorption tower so as to be reused therein as a regenerated amine solution. On the other hand, the CO 2 component released from CO 2 -rich amine absorbent solution, together with the steam, rises upward through air passages 20a between heat transfer plates 4a in the upper heat exchanger 2a. In this while, the gas passing through air passages 20a is cooled since cooling water is circulated inside the heat transfer plates 4a. Therefore, the steam component condenses on heat transfer plates 4a with nets 30 adhered thereto and flows downward slowly along the plates. The condensed water flowing downward, while exchanging heat with the cooling water inside the heat transfer plates 4a, comes into contact with (or performing gas-liquid contact with) the aforementioned gas rising upward from the lower heat exchanger 2b. Therefore, the gas rising is cooled by the gas-liquid contact whereby the amine component can be prevented from discharging outside the tower. In this way, also in the upper heat exchanger 2a, the gas-liquid contact and the heat exchange are simultaneously achieved highly efficiently. The gas rising upward and passing through the air passages 20a of the heat exchanger 2a is reduced in steam component and delivered to a next step as a CO 2 -rich gas. In the conventional regeneration tower, the gas mixture of CO 2 and steam delivered from the upper portion of the tower is cooled by a separately provided heat exchanger, in placed of the heat exchanger 2a of the present invention and the thus condensed water is sprayed from a nozzle at the top of the tower so as to prevent amine component from discharging outside the tower. Further, in place of the heat exchanger 2b, a part of regenerated amine is extracted from the tower and heated outside the tower to form steam, which is in turn fed to the tower bottom so as to strip off CO 2 component with steam (by steam-stripping) from the CO 2 -rich amine absorbent solution to thereby regenerate the absorbent solution. Thus, the conventional regeneration tower would require a separate heat exchanger and a heater outside the tower, complicating the structure of the apparatus. Moreover, the heat exchanging efficiency was not enough to satisfy the demands. In contrast, the use of the heat exchanger of gas-liquid contacting plate type of the present invention can execute both the gas-liquid contact and the heat exchange simultaneously, so that the structure of the chemical plant'can be markedly simplified and it is possible for the apparatus to run at high heat exchange efficiency. As has been detailed heretofore, according to the heat exchanger of gas-liquid contacting plate type of the present invention the contacting area between the gas and the liquid flowing downward along the heat transfer plates is increased by virtue of providing the nets. In addition, the nets hold the liquid so as to linger the staying time of the liquid that flows downward, so that the gas-liquid contacting efficiency is enhanced to a great degree with a markedly increased heat exchange efficiency. Further, the configuration of the apparatus can be made compact, so this feature contributes to save the space required for the plant to a great extent. The invention being thus described, it will be obvious that the same may be varied in many ways. Such variations are not to be regarded as a departure from the scope of the invention as defined in the claims, and all such modifications as would be obvious to one skilled in the art are intended to be included within the scope of the following claims.

Claims: A heat exchanger (2) of gas-liquid contacting plate type comprising: a plurality of heat transfer plates (4), disposed vertically at certain intervals, defining air flow passages (20) therebetween which allow air to rise, being characterized in that each of said plates (4) has a heat medium flowing passage (10) thereinside for allowing a heat medium (c) to flow therethrough and the side surfaces of each of said heat transfer plates, which define said air flow passages, are adhered with nets (30) for allowing a liquid to flow downward along the nets (30) and plates.

Inventors: FUJII MASUMI, HOTTA YOSHITSUGU, IIJIMA MASAKI, JINNO YUKIHIRO, KITAMURA KOICHI, MIMURA TOMOI, MITSUOKA SHIGEAKI, SHIMOJO SHIGERU, SUDA TAIICHIRO, FUJII, MASUMI, HOTTA, YOSHITSUGU, IIJIMA, MASAKI, JINNO, YUKIHIRO, KITAMURA, KOICHI, MIMURA, TOMOI, MITSUOKA, SHIGEAKI, SHIMOJO, SHIGERU, SUDA, TAIICHIRO, Fujii, Masumi, The Kansai Elec. Power Co. Inc., Hotta, Yoshitsugu, The Kansai Elec. Power Co. Inc., Jinno, Yukihiro, The Kansai Elec. Power Co. Inc., Kitamura, Koichi, The Kansai Elec. Power Co. Inc., Mimura, Tomoi, The Kansai Elec. Power Co. Inc., Mitsuoka, Shigeaki, Hiroshima Res. &amp; Dev. Center, Shimojo, Shigeru, The Kansai Elec. Power Co. Inc., Suda, Taiichiro, The Kansai Elec. Power Co. Inc.
Applicants: KANSAI ELECTRIC POWER CO, MITSUBISHI HEAVY IND LTD, MITSUBISHI JUKOGYO KABUSHIKI KAISHA, THE KANSAI ELECTRIC POWER CO., INC.
Application year: 1994
Main classification: F28D15
IPC codes: B01D53, F28D15, F28F13, F28D3